Control of catalytic processes using mobile catalysts



m. ...um momwm T. B. HUDSON 2,429,161

CONTROL 0F CATLYTIC PROCESSES USING MOBILE CATALYSTS Filed Aug. l. 1942 2 Sheets-Sheet 1 Oct. 14, 1947.

Oct. 14, 1947. T, B, HUDSQN 2,429,161

CONTROL 0F CATALYTIC PRGCESSES USING MOBILE CATALYSTS Filed Aug. 1, 1942 2 Sheets-Sheet 2 BF3 AND PROPANE MAKE UP BF3 AND 54 PROPANE REFRIGERAT PROPANE so\LvENT 6| POLYMER BE, a s oLvENT RECOVERY PROCESSES BUTENES SOLVENT FIG. 2

INVENTOR THOMAS B HUDSON Patented Oct. 14, 1947 CONTROL F CATALYTIC PROCESSES USING MOBILE CATALYSTS Thomas B. Hudson,

Bartlesville, Okla., assignor to Phillips Petroleum Company, a corporation of Delaware Application August 1, 1942, Serial No. 453,265

3 Claims. 1

This invention relates to improvements in catalytic processes. More particularly it relates to novel methods of bringing mobile catalysts into contact with reactants. It has particular relevance to organic reactions such as hydrocarbon conversions.

The use of catalysts has come to fbe of primary importance in industry. Catalysts may greatly accelerate the rate of reaction for many processes so that either a much more rapid conversion at a given temperature is obtained, or a much lower temperature may be used to accomplish a given conversion. In fact in many cases, catalysts of one kind or another have made possible the carrying out of reactions which previously had been believed impossible. While catalytic action cannot cause a reaction to occur which is thermodynamically impossible, it may be the only means of attaining a practical rate of reaction for a given conversion. Utilization of elevated temperatures frequently cannot be relied on due to shifts in equilibrium concentrations or due to the occurrence of undesired side reactions. Many reactions which will not take place at practicable temperature levels with any measurable speed, may occur almost quantitatively at reasonable temperatures in the presence of suitable catalysts.

In the hundred years since Berzelius first recognized the existence of certain reactions which were promoted by substances not changed during the reaction. and suggested the use of the term catalysis for describing the forces involved, the search for effective catalytic materials has commanded the attention of a great segment of the technical world. Since the turn of the century. the successful results of these investigations have given rise to numerous new industries, as well as providing greatly improved methods for the older industries.

The petroleum industry may be taken as one outstanding example. Whereas ten to twenty' years ago non-catalytic processes were '.tilized almost exclusively in all fields of petroleum refining, the trend now is toward catalytic processes, which are rapidly replacing older methods with results which are more satisfactory not only in increased efficiency but also in producing entirely new products. Present day needs call for highoctane gasoline, and various other fuels having special requirements. Aviation fuels in particular must now be prepared by blending almost pure individual hydrocarbons or hydrocarbon types in order to meet the demand for fuels which will readily respond to`specific operating conditions. Oishoots from the petroleum industry. such as the production of synthetic rubbers, call for preparing very pure single hydrocarbons for use as raw materials.

Not only is the chemical composition of the catalytic material of importance in attaining specific results in chemical conversions, but, its physical form, activation treatments. impurities. methods of contacting with reactants, reactivation processes, etc., all exert their infiuences on the source of the conversions being catalyzed. The particular products and yields thereof obtained are also dependent to a great extent on such reaction conditions as pressure, temperature, time of contact between reactants and catalyst, etc. Careful control o'f all these variables is required for production of the optimum quantities and quality of products. Organic conversions are particularly susceptible to the effects of these various factors, due to the numerous side reactions which can occur.

One of the most important influences on the course of catalyzed reactions, and frequently one of the most diiiicult to control, is temperature. Most of such reactions are either highly endothermic or highly eiiothermic, and maintenance of the desired range of temperature is a major operating diiiiculty. The activity of a catalyst for a definite conversion is usually of economic significance only within a fairly narrow temperature range, and a particular process using that catalyst must obviously be operated within the active range. This condition is shown by the great change in the degree of conversion usually occurring with relatively small temperature changes.

Thus, in the case of endothermic reactions, the temperature drop which normally occurs may be so pronounced that the rate of conversion will rapidly decrease to an uneconomic level. In the case of exothermic reactions, a rise in temperature normally occurs which, if not controlled in some way, will rapidly bring the temperature to a, point at which undesirable side reactions occur. In fact, such side reactions may frequently become the predominant reaction at temperatures only relatively slightly above those required for the desired conversions. Or, the principal reaction may be caused to proceed too rapidly. in which case the reaction rate and temperature become uncontrollable with undesirable or even disastrous results. Accordingly, the careful control of temperature within narrow limits throughout a reaction zone for either endothermic or exothermlc reactions is not only highly desirable but is ordinarily a necessity.

Many methods have been oiered for the control oi temperatures in catalytic conversions, usually involving complicated apparatus designs whereby indirect heat transfer is utilized in connection with portions of catalytic materials so small as to allow sumcient heat to pass from or into the catalyst mass to accomplish the desired results. For example, particles of solid catalyst have been packed into relatively small tubes so that no portion of the catalyst is more than say one inch from a tube wall, and a number of such tubes connected in parallel, with a heat transfer medium being circulated about the exterior of the tubes. An alternative method has been to provide a system of coils or the like within a catalyst mass so that a heating or cooling medium, as required, may be circulated throughout the catalyst bed. Similar arrangements have been provided for reaction vessels employing moving catalysts. However, these methods have not been able to compensate fully for the low thermal conductivity of the usual catalysts. Furthermore, the surface of tubes or other elements through which the heat transfer takes place, is at a temperature appreciably different from that generally prevailing in the reaction zone. This is disadvantageous, particularly with endothermic reactions where, in the case of hydrocarbon conversions for example, cracking, coke formation and other reactions take place on the superheated surfaces, which causes loss of materials and fouling of equipment.

Other methods proposed for compensating for heat of reaction include superheating of reactants involved in endothermic processes above optimum temperatures, or the converse, that is insufllcient preliminary heating of exothermic reactants. The inemciencies of such methods are obvious. Catalyst poisoning may sometimes occur to an increased extent at either lowered or increased temperature.

Probably the most common method of bringing solid catalysts into contact with reactants is to place the catalyst ln a reaction chamber, and pass the reactants therethrough at the desired ow rate, temperature, and pressure. However. in many cases, it has been found useful to cause the solid catalyst particles to move through the reaction zone. Also in the case of gaseous or liquid catalysts, the catalyst is frequently passed through the reaction zone. Such catalysts, whether solid, liquid, or gaseous, which are passed through a reaction zone, are referred to herein as mobile or fluent catalysts. They may be passed either concurrently with or countercurrently to the reactants, depending upon the reactions being catalyzed, the catalyst, and other variables.

Itis an object of this invention to provide novel catalytic processes. Another object is to provide improved methods of operating catalytic systems, particularly those employing mobile catalysts. Another object is to enable a more delicate control of catalyzed organic reactions. particularly hydrocarbon conversion. A further object is to provide improved methods of contacting mobile catalysts with reactants. A further object is to provide for the control of catalyzed reactions with respect to temperature and/or products btained. Yet another object is' to permit controlled variation in the quantity and/or activity of catalyst present at all points in a reaction zone. A still further object is to provide for the introduction of one or more catalysts intoy a reaction zone at a plurality of points. Another obiect is to provide for the concurrent or countercurrent dow of catalyst thus introduced relative to the ow of reactants. Another object is to correlate the introduction of catalyst with certain reaction conditions in an exact'manner so as to compensate, at least in part, for change in temperature and/or change in concentration of reactants, etc. A further object is to provide for reactivating catalysts which have become deactivated in such processes so that the reactivated catalyst may be re-introduced into contact with reactants. Other objects and advantages of the invention will become apparent from the following disclosure.

My invention is essentially a method for carefully controlling catalytic processes by the multipoint addition of catalyst, specically correlated with reaction conditions. Specific methods of operating are disclosed which are especially adapted for given types of conversions. These different methods, while each employing the introduction of catalyst into a reaction zone at a plurality of points, are not at all to be considered as exact equivalents inasmuch as each is particularly designed to give optimum results for the given application, as will be more fully explained. I am aware that catalytic materials have occasionally in the past been described as being introduced into a reaction zone at more than one point. Such disclosures, however, have been vague, indefinite. and most unenlightening as to the purposes involved and exact results accomplished. I have found specific relationships between catalyst introduction and reaction conditions, and have devised novel methods of correlating the various factors involved whereby new and highly useful results are accomplished, as will be apparent from the detailed teachings hereinbelow set forth.

From one point of view, the invention may be considered as comprising three principal operational modifications. A first modification has to do with catalysts which are miscible with one or more reactants, either by virtue or mutual solubility or because of small particle size of the catalyst allowing its suspension in reactants. Such a suspension may be in a more or less stable form, or in a relatively separable form in which the catalyst is maintained in suspension by means of turbulent flow, static charges, etc. Finely divided solid catalysts are frequently suspended in gaseous reactants and passed through a zone maintained under desired reaction conditions. Such catalysts have been called "fluid catalysts," which is in actuality a misnomer. However, they do often pass at the same rate of flow as the reactants and the entire mixture may be handled more or less as a single fluid. Accordingly, I may define fluid catalysts to include not only gaseous and liquid catalysts. but also finely divided solids suspended in reactants. A second modiflcation involve.; catalysts which are immiscible with reactants undergoing treatment, with the catalyst passing concurrently with the reactants through the reaction zone, generally at a rate different than the rate of ow of reactants. A third modification relates to catalytic materials which are non-miscible with reactants wherein the catalyst after being introduced at a plurality of points subsequently moves countercurrent to the reactants. In some cases there is a combination of the modifications, in which at least one reactant passes countercurrently to ,at least one other reactant, in which case the catalyst will more concurrently with one reactant and countercurrently to another reactant. R

The choice oi operating method, and the manner oi' applying that method, will of course be based on the type of catalyst, reaction, etc. However, the choice oi' points for introduction of the catalyst and the rate at which catalyst is introduced at each point is correlated with change in temperature. change in concentration of reactants, etc., so as to compensate for auch changes. as will now be more i'ully described.

By the use of my invention I may so interrelate the various factors such as temperature, flow rate of reactants, diluents, and catalysts, catalyst activity, time of contact between reactants and catalysts, etc., as to provide a most complete and delicate control over the nature and extent oi' reaction at all points in the reaction zone.

As pointed out above, temperature control is possibly the major problem in carrying out exothermic and endothermic reactions. The present invention provides methods for maintaining proper reaction velocity in the face of increasing or decreasing temperatures, or of avoiding such increases or decreases in temperature,

In the case of an endothermic reaction, the catalyst may be introduced at a plurality of points spaced in the direction of flow of reactants for concurrent flow therewith. 'I'he amount of catalyst is smallest in the rst portion o! the reaction zone, and largest in the last portion of the zone, due to the incremental additions of catalyst which occur along the path oi' ow. The temperature at the outlet of the reaction zone is considerably lower than at the inlet because the endothermal reaction takes up heat. The amount of catalyst added at each point is chosen so as to provide suiiicient additional catalytic activity to maintain the rate of reaction in spite of the lowered temperature existing at that point. Thus, even though under ordinary conditions the rate of reaction at a temperature, say 50 or 100 F., lower than the optimum reaction temperature would be several times less, resulting in much lowered conversion in the latter portions of the reaction zone, the additional catalyst compensates at least partially for the lowered temperature and may maintain substantially cons'tant conversion throughout the zone it added in sumcient quantity at each point.

Another manner of utilizing this invention for endothermic reactions involves multipoint addition of catalyst with subsequent countercurrent flow relative to the reactants. This may be done especially if the catalyst used undergoes very rapid deactivation at the given reaction conditions. In this case, the rate of introduction and ow of catalyst is regulated so that it is substantially spent, that is, deactivated for the reaction, by the time it exits from the reaction zone. The point of exit of catalyst is at or near the point of entrance of reactants. Accordingly, the reactants first contact a relatively large mass oi' substantially deactivated catalyst containing only a small proportion of active catalyst introduced at the later (earlier, with respect to reactants) points of the reaction zone. The total activity is quite limited, and smaller here than at subsequent points. As the reactants pass on through the zone, they contact smaller quantities of total catalyst, but the catalyst contacted has greater activity. The deactivated catalyst also has a diluent effect, and a unit volume of reactants passes through the ilrst portions of the reaction the endothermic nature oi' the reaction. The increments of catalyst added at the points ot lowest temperature may, ii' necessary, be larger than those added at the points oi' higher temperatures, the quantity added, rate of addition and rate of ow through the reaction zone always being so chosen and related as to compensate at least in part for the variation o1' reaction rate with temperature.

An exothermic reaction may be handled in a .somewhat diilerent manner, but with the same end in view, namely. the control of catalyst activity and contact time between catalyst and reactants so as to compensate, in part at least, for variation of rate of reaction with temperature. Generally, the most satisfactory control is obtained by use of countercurrent iiow of reactants and catalystvintroduced multipoint. Reactants first are contacted with a relatively large volume of catalyst, the ratio of catalyst activity to volume of reactants being greatest at this point and progressively decreasing in the direction of reactant flow, while the temperature correspondingly increases. At the higher temperature levels. less catalyst activity is encountered, so that reaction velocity may be maintained as nearly constant as desired. Near the exit from the reaction zone, the reactants are contacted with the smallest quantity of catalyst, this quantity, however, being suftlcient to maintain the desired rate of reaction. The advantages of operating in this manner may readily be seen by contrasting with prior methods wherein either the heat of reaction must be removed by difiicult means heretofore discussed, or, if the temperature is allowed to increase, contact with equal increments of catalyst combined with the higher temperatures causes greatly increased reaction rates.

Another method of controlling exothermic reactions which is particularly, although not eX- clusively adapted for use with catalysts which become rapidly deactivated. is the concurrent flow of multipoint-introduced catalyst. In such usage, a rst portion of catalyst is introduced either along with the reactant feed or separately into the reaction zone near the point of entrance of the reactants, and the next portion of catalyst, generally smaller. is added at a point at which the first portion is mostly deactivated; at any rate, the relationship of the amount of catalyst thus introduced to the extent of deactivation of previously introduced catalyst is such that the ratio of total catalyst activity to volume of reactants at that point is less than at the earlier point of catalyst introduction, the difference being generally inversely proportional to temperature. It would not be at all desirable to introduce catalyst increments of equal activity at equal points while the temperature is rising. As the temperature increases in the direction of flow of reactants, the catalyst activity decreases so as to avoid a constantly increasing conversion rate as would normally be encountered.

The above discussion is directed towards processes carried out under adiabatic, or at least partially adiabatic conditions in which the heat oi amarsi reaction causes a temperature gradient in exist along the direction of now of reactants. A oomblnation of indirect heat exchange to partially overcome heat of reaction, with the controlled introduction of catalyst as described above, may be used for exothermic or endothermic reactions.

In case it is desired to maintain substantially isothermal conditions in endothermic or exothermic reactions by means or indirect heat exchange or other methods. this invention may be utilized to obtain a more satisfactory control of reaction and to simplify the temperature control. When reactants are passed through a stationary bed of catalyst, or contacted with a single portion of mobile cataLvst. there is a tendency for the reaction to proceed too rapidly at nrst, with consequent overheating or cooling, as the case may be, at the rst point of contact between reactants and catalyst and too rapid catalyst deactivation at that point. However, by adding catalyst to the reaction zone in controlled increments in accordance with my invention, the extent of reaction and temperature may be maintained under strict control since reactants are contacted with a. limited portion of catalyst. and are not contacted with an additional portion until the temperature is brought back to the .desired value. The catalyst is not added haphazardly, but the addition is carefully correlated with the amount of heat produced or consumed by the reaction and with the amount removed or introduced, so as to avoid localized spots of overheating or excessive cooling. Catalyst and reactants may now countercurrently or concurrently, depending upon the type of reaction, catalyst, etc.. the proper modiiications being readily chosen in view of the detailed disclosures oiered herein.

Other operating problems frequently encountered in catalytic reactions involve catalyst deactivation and means for avoiding same or for reactivating catalyst, the activity of which has dropped to an uneconomic level. Mobile catalysts are generally subjected to reactivation treatment either after each passage through a reaction zone. or a portion only may be treated each time to keep the overall activity at the desired level. One of the advantages of mobile catalysts-over stationary catalysts is that control of regeneration is thus obtained in a fairly simple manner. However, only the overall activity is thus aiiected, the actual activity at any particular point in the reaction zone being dependent upon conditions therein which are not readily changed with respect to deactivation of catalyst which is occurring. For example, many catalysts will be subjected to a rather extensive deactivation in a relatively small rst portion of the reaction zone, due to temperature conditions. poisons, etcl, with deactivation in subsequent portions of the reaction zone continuing at a much slower rate. In such a case, it will be seen that while the average or overall activity may be regulated, the uneven loss in activity causes an ineflicient operation.

My invention provides a means for controlling the activity of mobile catalysts at any point in a reaction zone. This may readily be accomplished by controlling the quantity and/or activity of catalyst introduced at the dierent points. Thus in certain cases, partially or completely deactivated catalyst may be admixed in varying proportions with iresh or' reactivated catalyst to give the desired activity for introduction at any particular point. In fact. in some cases more than one different type of -catalyst may be used for introduction at diierent points into a single reaction zone to give controlled activity. which may be either maintained constant or varied trom point to point to meet the needs of the particular reaction being catalyzed. Examples given herein will serve to point out more clearly a few oi the many ways in which controlled variation or constant activity of catalyst is obtained and correlated with other reaction conditions through use of this invention.

Another method by which my invention makes possible a more effective use of catalyst is by controlling the quantity and/or activity of mobile catalyst in a reaction zone in relation to the concentration of reactants existing at various points in the zone. The change in concentration of reactants in a reaction zone depends upon the extent of conversion occurring. If, as in many cases, a substantially complete conversion of reactants to products is desired by the time the reaction mixture leaves the reaction zone, it will be seen that the concentration of at least one reactant must approach zero at the reactionzone exit. In many other reactions, however, an equilibrium may exist which prevents, or economic considerations may make undesirable, a complete conversion. 'Ihe extent of conversion may vary greatly with the type of reaction being catalyzed, one process involving say a one per cent conversion per pass While another may accomplish forty, sixty. or more per cent conversion in one pass. Ordinarily in case the percentage conversion is low, the loss in concentration of reactants as the reaction proceeds does not greatly aiiect the reaction rate. However. in the case of higher conversions ranging on up to per cent, the lowered concentrations of reactants existing in the latter parts of the reaction zone may greatly decrease the reaction rate, even though expedients such as using a large excess of one reactant or the like are resorted to. By controlling the multipoint introduction of catalyst in accordance with the decrease in reactant concentration, I may partially or completely compensate therefor, and avoidtoo great or any decrease in reaction rate by providing more catalyst activity at the points of lower concentration. The dilution eilect oi' the catalyst is also to be considered. Again. the catalyst may pass either concurrently or countercurrently to the reactant depending upon the various factors involved for any particular reaction.

It is to be understood that the various methods of utilizing the present invention, that is, for

e example, by controlling the introduction of catalyst to compensate for changes in temperature. catalyst activity, reactant concentration, etc., may be used either alone or in various combinations, one with the other, as will be well understood by one skilled in the art in view of the full and complete disclosure given herein. Obviously the choice of one or a combination of methods of operating will have to be made with due consideration for the reactions being catalyzed. the type .oi' catalyst most suitable, the extent of reaction. the thermal changes involved, the necessities and possibilities of applying reactivation processes to the catalyst, etc. Various modications such as introducing diluents, refrigerants, heat carriers. reactants, and the like, multipoint along with or separately from the multipoint-injected catalyst. may be used as found advantageous ior any particular process.

A numerical treatment may be used at this point in order to bring out more clearly the hereinbefore discussed principles upon. which the invention is based. A number of assumptions will be made to eliminate variable and simplify the presentation. A simple example would be an endothermic conversion involving heterogeneous catalysis, for example the conversion of an organic fluid using a solid contact catalyst in inely divided form. The data below will show how the invention is utilized to maintain a constant reaction rate by overcoming the eii'ects of decreasing temperature, decreasing concentration of reactants. and any deactivation of the catalyst. which would, if the invention were not used but the same total conversion were obtained, cause the reaction rate to drop to a value in the last part of the reaction zone equal to only one-sixth that at the ilrst part oi' the reaction zone. Assume no change in volume of reactants upon reaction, and assume that doubling the number of particles of catalyst will cause twice as much reaction to occur in a given time due to the doubled area of catalytic contact surface offered the reactants. Let a cylindrical reaction zone through which reactants and catalyst flow concurrently at the same rate be considered as divided into six cylindrical increments of equal volume referred to hereinafter as unit volumes. Let 0.5 unit volume of reactants enter one end of the reaction zone per minute, and a total of 0.5 unit volume of catalyst enter the zone per minute in equal increments of 0.083 volume at each of six equally spaced points; that is, 0.083 volume of catalyst is introduced into each of the six aforementioned incremental unit volumes of the catalyst zone'. In the rst unit volume of the reaction zone, the ratio of volume of catalyst to volume of reactants is 0.083 0.083 1-o.o83 oT7='09 in the sixth and last unit volume of the reaction zone the ratio is Thus the ratio of catalyst to reactants at the outlet is if 11 times that a the inlet and accordingly, the effect on the reaction rate would be to increase the rate 11 times. Considering now the contact time, it will be seen on following 0.5 volume of reactants through the catalyst zone that it requires -5- 1.83 minutes to traverse the first unit volume of the zone and that is, the conversion would be approximately halved. Taking the two effects of contact time and ratio of catalyst to reactants, the overall tendency toward change in conversion would be approximately expressed as 1.0 1.00 coaxs-a'l 'I'hese figures indicate quantitatively the tendency toward increased reaction rate caused by the multipoint introduction of catalyst in the exact mannenjust described, which tendency may be used to maintain a substantially constant overall reactlon rate by counteracting the effects of such changes in reaction conditions as drop in temperature due to the endothermal nature of the reaction and/or decrease in concentration of reactants, etc., to the extent that any of such changes in conditions, or the effect of all combined, tend to cause a six-fold decrease in reaction rate. In similar cases in which the depressing influences on the reaction rate are greater or less than six fold, the rate would be held constant by a corresponding increased or decreased overall ratio of catalyst to reactants, or by a controlledgchange in the activity of catalyst introduced at succeeding points, etc.. the exact conditions being calculated in a. manner similar to that shown above. Application of this type of procedure to a specific endothermal reaction will be described in more detail hereinbelow with reference to Figure 1. In order to explain the invention more fully, the following examples and appended drawings are provided to illustrate specific embodiments of the process, but no limitations are thereby implied. inasmuch as the invention may be utilized in numerous other manners by following the teachings of this disclosure.

Figure 1 shows in diagrammatic form an arrangement of equipment for carrying out the catalytic ,cracking of petroleum oils. an endothermic reaction, using a nnely divided solid catalyst suspended in vaporous reactants and thus flowing concurrently therewith, commonly termed a fluid catalyst" process.

Figure 2 shows diagrammatically apparatus for polymerizing butenes, an exothermic reaction, in which a gaseous catalyst immiscible with the liquid reaction mixture is passed countercurrently to the reactants.

Figure 3 is a. diagrammatic drawing of apparatus used for the vapor phase reduction of nitrobenzene with gaseous hydrogen. an exothermic reaction, wherein a. metal catalyst supported on a solid granular carrier material is passed concurrently with, but at a diiIerent rate than. the reactants.

In Figure l. the reactant, for example gasoil derived by straight-run distillation of crude petroleum, passes from line I0 into blower il, and thence through line I2 into heater I3 wherein it is raised to a suitable temperature such as 900 F. for the initiation of the reaction upon contact with the catalyst. From heater I3 the heated reactants are sent through line Il into the reaction chamber I 5. This reaction chamber may take the form of an elongated tube, as shown diagrammatically in Figure 1. Various types of reaction chambers suitable for use with powdered catalysts are known in the art. A very nnely divided solid catalyst is injected into reaction chamber I5 at spaced points along the path of flow of reactants through lines I6, I1, i8, and I9. Obviously, although only four lines are shown, the number of such lines may be varied at will to obtain suitable operating conditions compatible with economy of equipment. The catalyst may be of the natural clay type such as fullers earth. bentonite, etc., preferably activated in known manner. or of the synthetic type such as silica-alumina or other eiiective catalysts known to the art. The method of introducing the iinely divided catalyst into the reaction zone may include such operations as suspension in liquid or gaseous reactants or diluents.

The catalyst may enter lines I6, l'l, i8, and I9 from two sources. The first source is conduit which carries recycled catalyst which has been partially deactivated by previous use in the process. The second source is conduit 2| which carries regenerated catalyst from catalyst regeneration zone 22. Carbonaceous deposits are removed from the catalyst in zone 22 by burning in an oxygen-containing gas. The quantity of catalyst from each source injected at each point is regulated by suitable means so that all oi the catalyst entering through line IG is the partly deactivated catalyst from conduit 2li; most of that entering through line I1 is of the same type, but has admixed with it by means oi line 23 a small portion of freshly regenerated catalyst from conduit 2l; that entering through line I8 has a larger proportion of reactivated catalyst, which reaches line i8 through line 2|; and thatentering at the last point through line I9 is composed entirely of regenerated catalyst from conduit 2|.

The mixture of products, excess reactants if any. and catalyst passes from reaction zone Il through conduit 25 into a catalystseparation' zone 26. which may be a cyclone separator, electrical precipitator, or any other suitable means for accomplishing the separation oi' finely divided catalyst irom the hot vapors. Catalyst passes from zone 26 into conduit 21 and a portion is taken from conduit 21 through conduit 28 to the catalyst regeneration zone 22. Vapors leave the catalyst separating zone 2B through line 29, and may be condensed and fractionated to separate out the desired cracked gasoline product, with unreacted gas-oil being recycled to the reaction chamber. If desired, various other niodiilcations o! such a cracking process. which are known to the art, for example recycle of very small amounts of hydrogen. etc., may be used.

The cracking of lpetroleum oils is an endothermic process, and, as heretofore explained, under ordinary methods of operation a substantial temperature drop occurs which causes a decrease in reaction rate as the reactants proceed through the cracking zone. However. by controlling the relative volumes of partially deactivated and of activated catalyst and also the total volumes of the catalyst introduced into the reaction zone as just described, in conformity with the principles heretofore discussed in detail, the total catalytic activity at each succeeding point in the cracking zone in the direction o! flow of reactants is greater than the activity at the preceding points, the increase in activity being such that the normal decrease in reaction rate accompanying dropping temperatures and catalyst deactivation is partially or completely obviated. This increase in total catalyst-activity is obtained by the increasing volume of catalyst due to its multipoint introduction, and the increasing activity of the catalyst introduced. due to the use of relatively greater proportions of freshly reactivated catalyst in the increments introduced along the path of ow oi' reactants. Of course, the actual quantities 0I catalyst ig? 12 trcduced at the various points will depend upon the catalyst being used. its rate of deactivation under the given reaction condition. rate of ow of reactants and catalyst. extent of reactivation effected in the catalyst regeneration zone, the characteristics of the gas-oil being cracked, temperature and pressure conditions in the cracking zone, extent of indirect heat exchange occurring between the cracking furnace and any outside sources of heat, or cooler surroundings, etc. this disclosure will readily enable one skilled in the art to correlate these various factors for any particular application to obtain the advantages of the invention. Although in the drawing the rst point of catalyst introduction into the reaction zone is shown past the reactant inlet. this iirst point may also be positioned at or just before the inlet so that the first increment of catalyst enters along with the reactants.

It will be noted that in the cracking process as shown in Figure 1, several of the aspects of my invention which were described before in some detail may be involved. For example, the endothermic nature of the reaction will. unless sufficient heat exchange is provided, cause the temperature to drop. The multipoint introduction of catalyst is so controlled as to counterbalance this eifect in order to maintain desired reaction velocities. The catalyst during its travel through the cracking zone becomes at least partially deactivated, thus tending to slow the reaction even at constant temperatures. Ad ditional catalyst, including regenerated catalyst, is introduced in such quantities as to compensate for the deactivation occurring in the cracking zone. Another factor tending to decrease reaction rates in the decrease in concentration of reactants which occurs as the reactionp'roceeds. Since in a gas-oil cracking process of the type described, only partial conversion, say from l5 to 40 per cent, is permitted to occur in one pass, the decrease in reactant concentration does not iniluence the course of reaction so much as in the case of reactions giving complete conversion in a single pass. However, any effect of this kind is readily overcome by the controlled addition of ,catalyst at the different points along the cracking zone.

Thus it is seen that in a typical process, gas-oil cracking, control of catalyst addition may be related to several variables. On the other hand. well known expedients might in some cases be utilized to control'certain of these variables. For example. sufficient heat may be introduced into the cracking zone by various means as to maintain asubstantfally constant temperature, although this is diillcult to accomplish in actual practice. points would be controlled to make up for the combined effects ci loss in catalyst activity and change in reactant concentration. On the other hand, reaction conditions may be maintained which are So mild that the amount of catalyst deactivation occurring in a single pass will be very slight, so that the principal purpose of introducing the catalyst at points will be to compensate fcr decreasing temperatures and/or concentration of reactants in order to maintain a substantially constant reaction rate.

In Figure 2, an elongated reaction chamber Il is provided, the interior of which may be filled with packing material for promoting intimate contact between gases and liquids. Fed to the system through line 4I is a gaseous hydrocarbon However. the general principles set out in- In such a case, catalyst addition at mixture containing a substantial proportion of butenes, preferably isobutylene although normal butenes may also be present. This gas is compressed in compressor 42 and then passes via line 43 to heat exchanger M where it is cooled by indirect exchange with effluents from the reaction chamber. From the heat exchanger the cooled hydrocarbons pass via line 45 into the top of reaction chamber 40, wherein they are subjected to the polymerizing action of boron triiluoride (BFa) as hereinafter described. Refrigeration means 46 is interposed in line 45, and serves to cool the reactant feed to the desired reaction ternperature, in this case 30 C. The hydrocarbons making up the feed are in liquid phase at this temperature, and the reaction chamber is operated at substantially atmospheric pressure.

Ordinarily a C4 fraction is used which contains substantial amounts of butanes, which serve as a diluent and as a solvent for the high molecular weight polymers formed in the reaction. If such butanes are not available admixed with the butenes, they may be supplied, or pentane or other suitable saturated hydrocarbon solvent may be used. The liquid butenes and accompanying hydrocarbons flow downwardly in chamber 4I) countercurrent to gaseous BF3 and gaseous propane, and substantially complete polymerization of the butenes occurs to form polymers of a molecular weight suitable for use as lubricating oils, additives to oils, etc.

The boron uoride catalyst passes from conduit 41 into reaction chamber 40 at a plurality of points by means of valved lines 48A-48G inclusive. Also introduced into chamber 40 at the same points is liqueiied |propane from conduit 49 via valved lines SDA-50G inclusive. This liquid propane acts 'as a coolant, diluent, and dispersant for the BFa, as will be explained in more detail below. Ordinarily a catalyst activator such as hydrogen fluoride, or other materials which will cause the production of hydrogen halides in the reaction zone, is introduced in small amount along with the boron fluoride or otherwise. Furthermore, metallic nickel or other metals are occasionally used in the reaction zone to help catalyze or promote the reaction.

'I'he butenes upon first entering chamber 40 and beginning their downward flow therethrough come into contactl with a gas phase which comprises propane and BFs. The volume of the gas phase is greater at this point than at any other point in the chamber. Polymerization is initiated by the catalytic action of the boron fluoride. This polymerization reaction is highly exothermic, and the temperature must'be held under very careful control, particularly since the type of product obtained may change greatly with a relatively small change in temperature; that is, the product formed at 30 C. may have an average molecular weight several times that of the product formed at C. For this reason, it is preferred to carry out the reaction as nearly isothermally as possible. l

The amount of boron fluoride introduced will ordinarily vary from point to point. being smallest at the top point (conduit 48A) and greatest at the bottom point (conduit MG) By this multipoint addition of the catalyst. a much more eilicient reaction control is realized, since the reactants do not contact the total amount of` catalyst at once. The catalyst contacted at the ilrst point comprises not only that introduced through conduit 48A, but also any bubbling up from the lower part of the reaction chamber. Just enough is introduced through line 48A to furnish sumcient fresh catalyst to initiate the reaction to the desired extent. It will be seen that the downward-ilowing reaction mixture continuously contacts upwardly flowing catalyst. Due to the formation of complexes between boron uoride and olens, a substantial part of the catalyst combines with reactants and is carried down as complex, Such complexes have only a llmited amount oi catalytic activity, if at all. Thus, if all the catalyst were introduced at the bottom, it would be continuously reacting with olens as it rose through the chamber, and the upper part of the chamber would be deficient in catalyst. In order to ensure that some catalyst rea-ches the top of the chamber, an otherwise unnecessary excess would have to be introduced at the bottom. Much better results are obtained by the multipoint addition, by which each increment added to the gas phase flowing upward through the reaction chamber can be controlled in amount to give just the desired concentration of catalyst at; the given point. It is preferable that the amount of catalyst be relatively small at the top of the chamber where the reaction starts, since the major part of the reaction and thus heat evolution generally occurs in the upper half of the chamber where the greatest concentration of monomers is found.

The introduction of controlled amounts oi.' cold liquid propane at points along with the catalyst gives effective control of temperature throughout chamber Il). The propane vaporizes immediately upon entering the chamber, and in so doing absorbs the heat of reaction. Of course, additional indirect heat exchange may be provided for chamber lllto assist in removing the heat of reaction if desired, particularly in order to avoid having too large an amount of gaseous propane passing through the reactor. A convenient way to do this is to pass chilled liquid propane through coils in chamber Il) in indirect heat exchange with the reactants, and then to pass the desired amount oi' the propane into conduit I9 for direct introduction through conduits 50A, 50B, etc.

Since the amount of BF: used is only a small percentage of the hydrocarbons charged, say from 0.5 to 5.0 mol per cent, the propane gas is very eective in promoting a more thorough dispersal of the catalyst throughout the reaction zone. It also serves as a diluent both for the liquid reactants and for the gaseous BFa. For this reason, larger amounts of BF; may be passed through reaction chamber I0 thus admixed with propane than would be suitable in the absence of the added gas. This excess BF: is recovered and recycled. The amount of liquid propane added through the lower conduits, for example, NG to BUF, is less than that added through the upper conduits such as 50A and 50B. This is because more heat of reaction is developed at the top of chamber 40 than at the bottom, and more evaporation of propane is needed at the top to maintain the desired low temperature.

Flow rate oi' reactants through chamber 4I! is preferably such that substantially no unpolymerized butenes are present in the efiiuents and the polymers in the etlluents are predominately of high molecular weight, for example over 2000. The character of the polymers can be controlled to a certain extent by controlling the reaction time and thus the extent oi' conversion, although a change in operating temperature will generally have more influence on the final product. A short conversion time will ordinarily produce some oi' the high molecular weight polymers, with a larger percentage of intermediate polymers which may be used for dierent purposes or which may be recycled to reaction chamber 40. The volume oi propane gas passed through reaction chamber 40 will generally be several times the volume of liquid reactants andsolvent passed through the chamber in a given time.

Propane gas and boron fluoride gas leaving the top of chamber Il! via line I are compressed in compressor 52, chilled, by partial evaporation in known manner, if desired, in refrigeration means 53 to condense liquid propane, and then passed to accumulator 5l. Cold gaseous boron iluoride leaves the top of accumulator 54 through line l1 for re-use in the process, while cold liquid propane leaves the bottom of accumulator 54 by line I9 to be introduced into chamber lll as described above. Of course, the gas phase from accumulator 54 contains some propane, and the liquid phase contains some boron iluoride in solution.

Since butenes are appreciably volatile at the temperature oi operation of chamber lil, the gas leaving that chamber via line 5I has some butenes in it., and these butenes tend to undergo some polymerization in line 5 Land compressor 52. For this reason, it is desirable that the length o! line 5l between chamber 50 and compressor 52 be short, and that the line 5I and compressor be flushed periodically with a solvent for the polymers such as liquid butane. Not much trouble is experienced from compressor 52 on, since iquid propane is present which acts as solvent. The amount oi polymer formed is small compared to the amount of butenes passing through this part oi' the system, most of the butenes returning unchanged into reaction chamber Ill along with the propane. A very satisfactory way to obviate any difliculty in this regard is to wash the gas in line 5I with suilicient liquid butane or pentane to remove practically all oi the butene. The liquid may then ilow directly into chamber lli. Thisl modication is not'shown in the drawing for the sake of simplicity.

Liquid products leave the bottom of reaction chamber Il) through line 55 and pass through heat exchanger 4l to be warmed to a higher temperature and to cool the incoming butenes. From exchanger 4l the products pass via line 56 to separator 51 wherein dissolved and/ or entrained boron fluoride and propane gas are evolved,

which pass via line 5B to line 5l for recovery and re-use. Liquid products pass from separator 51 via line 59 to boron fluoride and solvent recovery means which are indicated dia grammatically at GII. The solvent, which ordinarily is butane, is recovered by evaporation and leaves the system through line 6I. Part or all of the solvent may of course be recycled to line 4| or elsewhere if desired. Boron fluoride is recovered from its complexes by heating or other means, and is returned to the system by lines 52. 5l. and 5l. Ordinarily heating the product to 125 C. or higher will serve to release at least part oi the boron iluoride from the hydrocarbons. Polymer is removed from the system at 63. Any make-up BF: and/or propane required may be supplied through line vB4.

The above-described process exemplifies an adaptation of my invention to a highly exothermic reaction wherein the temperature is maintained constant. The multipoint addition of catalyst is controlled with respect to two principal variables. One is the loss of catalyst by complex formation. Catalyst is added at points to main- 16 tain the desired amount ot active catalyst. The other is change in concentration o! reactants. The smallest concentration oi catalyst is maintained at the point ot greatest concentration ot butenes, while the greatest concentration o! catalyst is at the outlet where reaction is being completed with practically no butenes remaining. It is to be noted that due to the diluent effect of the gaseous propane, the actual quantity of catalyst may under certain conditions be greater at the top point than at the bottom point, but the ratio oi catalyst activity to reactants decreases from bottom to top, the diluted catalyst having less eiiect than the undiluted catalyst. The catalyst activity thus changes in relation to the extent oi reaction, to compensate at least in part for the tendency toward decreased reaction rate.

An important aspect of the polymerization process as described is the fact that, while actual cooling is accomplished by the propane, temperature control is effected to a large extent by the multipoint addition or the catalyst. This is because the rate of addition o! catalyst at each point is so controlled and correlated with the other factors that catalyst activity at the point of greatest tendency toward heat evolution, that is the butene inlet. is smaller than at any other point, and the catalyst activity is increased as the tendency toward heat evolution decreases. The entire process may be contrasted with the prior 4art methods wherein the boron fluoride is added all at one point with consequent violent reaction at that point with little or no reaction at other points or wherein ineillcient batch methods are employed with vigorous stirring, gradual addition of catalyst and/or reactants is resorted to, and the reaction time is unduly extended because of the inherent limitations of that method of operating.

In Figure 3, the reaction chamber 1|I is preferably provided with means (not shown) for removing at least most of the heat of reaction by indirect heat exchange. A certain amount of heat is also lost to the atmosphere, but in order to avoid uneven cooling the entire chamber is ordinarily provided w'lth some insulation. Heated vaporized nitrobenzene from line 1| and hydrogen from line 12 join in line 13, and ilow into reaction chamber 10 i'or downward ilow therethrough. The hydrogen may be admixed with substantial amounts of carbon monoxide, or with inert gases such as methane or nitrogen. In fact,

in carrying out the reduction of nitrobenzene in l accordance with the present invention, I prefer to have some inert gas with the hydrogen. The ratio of hydrogen to nitrobenzene must be held within relatively narrow limits to obtain the highest yield oi aniline, since a ratio considerably higher or lower than the stoichiometrlcal amount gives rise to reduction products other than aniline. It is best to have somewhat more than the theoretical ratio of hydrogen to nitrobenzene, but not too much more, in order to ensure completion of the reaction, and some inert gas is preferably used in admlxture with the hydrogen.

A suitable supported hydrogenation catalyst in granular i'orm is caused to pass through conduit 14 into manifold 15. Branching oil from manl- Iold 15 are branches 15A-161i' inclusive through which the catalyst is introduced into the reaction chamber 1|! at spaced points along the path of flow of reactants. The quantity of catalyst introduced through each branch 18A, etc.. may be controlled by any suitable means. It will be 17 appreciated that due consideration must be given to the fact that chamber 1I is operated under pressure. The lines, 'IIA to 1I? inclusive, are shown equally spaced: however, the lines may be more or less in number. and evenly or unevenly spaced, in accordance with the capacity of the system, convenience oi' fabrication, operating conditions, rate o! catalyst introduction at the various points, and economy of equipment. A series oi bailes 'I1 vis provided in chamber 1I to keep the catalyst particles dispersed and in good contact with reactants as the catalyst falls to the bottom of chamber 1l. These bailles preferably have only a slight inclination from the horizontal so that catalyst is more or less pushed oi! oi' one baille down to the next by incoming catlyst.

In the hydrogenation of ntirobenzene by prior methods, the reaction mixture is passed through a stationary bed of catalyst. Since the concentration oi reactants is greatest in the nrst portions oi the catalyst bed, the major part of the reaction occurs bei'ore the bed is halfway traversed. This means that the amount oi heat liberated in the upper parts of the catalyst chamber is greater than in the lower parts. and thus the load on heat exchange coils or the like with which the chamber may be provided is greatest at the top and least at the bottom. Thus the heat exchange means must either be oversized at points or is overloaded. In practical operation, the heat of reaction cannot be satisfactorily removed, and a serious temperature rise occurs.

This is very undesirable, since the optimum yield of aniline, when using any given catalyst, is obtained only in a relatively narrow temperature range. Sintering of catalyst is also likely to occur on the most active catalytic points where the actual temperature may be from 25 or 50 to a hundred or so degrees centigrade higher than the mean temperature of the reactants and catalyst near those points. A further disadvantage lies in the fact that the temperature rise serves to increase the already excessive reaction rate still more.

By means of my invention the catalyst addition is controlled in accordance with the rate of reaction or rate of evolution of heat, so that substantially equal, or at least regularly varying quantities of heat are evolved and removed 4along equal increments oi' the length of reaction chamber lil. Thus, in the rst part o! reaction chamber 10, a relatively small amount of catalyst is introduced through branch 16A. Since the highest concentrations of nitrobenzene and of hydrogen are found in this portion of the reaction zone a small amount of catalyst is sufficient to promote considerable reaction. As the reaction rate tends to lessen due to the diluent effects of the anlline formed, or stated another way, due to the lowered concentrations of nitrobenzene and hydrogen, additional catalyst enters the reaction zone through lBB, and the reaction rate tends to increase again. Thus, the quantity of active catalyst surface present at various points in reaction chamber 'lll is maintained suillciently, as the reactants now therethrough, so as to give a completely reduced product in the eilluents. The amount of catalyst in the parts of chamber 'Il is small at the inlet thereof, and increases gradually toward the outlet, where Vit reaches a maximum. The reaction rate is maintained more or less constant throughout the reaction zone, in contrast to other methods wherein the last half of the catalyst chamber may be used for eiect- 18 ingolvfiveortenpercent ofthetotalccnversion. The temperature may be maintained substantially constant due to the fact that the amount of heat liberated is not excessive at any point, or a gradual temperature gradient may be allowed to exist, an increase of say 50 C. from the inlet to the outlet being permissible without undesirable eilects. It is to be noted however, that in using my invention, such a temperature gradient is regular, and is obtained gradually as the reactants ilow through the apparatus, rather than being obtained all at once as by other methods, in which case a peak teme perature may even occur, with a subsequent falling oil' in the latter stages where very little reaction is occurring.

A certain amount ot catalyst deactivation will occur which tends to lessen the reaction rate, and this is also compensated ior by the fresh catalyst added. The rate of catalyst deactivation will of course depend upon the catalyst used. the severity of reaction conditions. and particularly upon the purity of the reactants. Generally, the amount oi catalyst poisons present in the nitrobenzene and hydrogen las is small, and catalyst deactivation is not of great consequence in lessening the reaction rate in the passage of catalyst from one point to the next in reaction chamber 1li. The relative rates at which catalyst is introl duced at the various points will be determined as described above with reference to control of rate of reaction, while the total rate of catalyst flow into and thence out of chamber 1l will generally be chosen with respect to the type of reactivation treatment to which the catalyst is subjected outside the chamber. It is usually preferable to reactivate the catalyst before it has lost too much of its activity, since considerably higher temperatures frequently must be used in the reaction zone with a less active catalyst. Thus it is seen that a continuous now of catalyst is maintained through chamber lll so that the catalyst as removed trom the bottom thereof is usually still fairly active. The rate of ilow oi gaseous reactants through the catalyst chamber 'ill will be many times greater, on a. volume basis, than the rate of now ot catalyst therethrough.

The total eiliuent from reaction chamber 'I0 passes out through conduit 1B and then to catalyst separator 19 where the catalyst separates from the gases by gravity. This catalyst is removed through conduit containing suitable conveying means such as screw Il. From 8|! the catalyst passes through conduit 82 to conduit 'il for re-use in the process. A portion ot the catalyst stream may be continuously by-passed through a regeneration zone indicated diagrammatically at B3 to maintain the total catalyst stream at the desired activity. The regeneration in zone 83 comprises conventional chemical treatments to remove accumulated impurities and to restore the catalyst to substantially its original conditions. The entire stream of catalyst, rather than a portion, may be passed through regeneration zone 8l if desired.

The gases in catalyst separator 19 comprise aniline produced in the process, any traces of unreduced nitrobenzene, steam formed as a by-product, any excess hydrogen, and any inert gas introduced along with the hydrogen. This gas phase is passed via line u through cooler B5 and into product separator 86, wherein a liquid waterrich phase, a liquid aniline-rich phase, and a gaseous phase separate out. The gas is recycled via line 81 to line 12 for re-use of the hydrogen in the process. In order to prevent inert gases from pyramiding in the system, a portion of the gas is allowed to leave line 81 through valved branch I8. The aniline is removed from separator B6 through line 88 and passed to suitable apparatus for removing dissolved water and any other impurities. Water is removed from separator Bi through line B0, and passed to a system for recovering dissolved aniline therefrom. One very eii'ective method oi accomplishing this is to extract the aniline from the water with nitrobenzene, the extract then being led to the reaction zone for reduction of the nitrobenzene.

Suitable catalysts for the reduction of nitrobenzene according to the system Just described may comprise metals such as gold, silver, nickel, copper, or tin, either alone or in admixture, and preferably supported on granular carriers such as pumice, porcelain, alumina, etc. It is necessary that the catalyst composition have suillcient mechanical strength for withstanding the effects of continuously moving through the equipment. A preferred catalyst comprises supported tin prepared from the precipitated hydroxide or `carbonate. With such a catalyst, an operating temperature in reaction chamber 1li in the range of about 275 C. to 375 C. is suitable.

Various modes or operating have been disclosed herein, along with the broad concepts involved, so that one skilled in the art may, by suitable simple modifications, apply the principles of my invention to conform to the economic and practical considerations which will vary somewhat with each particular material treated. By following the teachings of my invention, the contacting of catalysts with reactants may be so exactly correlated with reaction conditions as to give a well regulated operation not heretofore taught. While I have disclosed certain speciiic processes, with particular reference to petroleum conversions, I do not wish to be limited to the exact modifications described, but only by the appended claims.

I claim:

1. A process for the 'catalytic cracking of petroleum oil into lower-boiling products which comprises vaporizing said petroleum oil, passing the resultant vapors through an elongated reaction zone at cracking conditions of temperature and pressure, such that the temperature decreases in the direction of ow due to the endothermic reaction, introducing powdered cracking catalyst from two sources as hereinafter described into said reaction zone at a plurality of points spaced in the direction of flow for suspension in said vapors, separating said lower-boiling products from the eflluents of said reaction zone, separating and recycling insufficiently converted oil, separating substantially all of the catalyst so introduced from the eiuents of said reaction zone, the thus-separated catalyst still retaining some activity, reactivating only a portion of said separated catalyst, recycling the remainder of said separated catalyst without reactivation to a plurality of said points including the iirst and excluding the last of said points in the direction of flow, the unreactivated catalyst introduced to said rst point being the sole catalyst introduced thereto and a diminishing quantity of unreactivated catalyst being introduced at each succeeding point in the direction of ow. introducing the reactivated portion of said catalyst into the reaction zone at a plurality of points excluding the ilrst and including the last of said points in the direction of flow, the reactivated catalyst introduced to said last point being the sole catalyst introduced thereto and an increasing quantity of reactivated catalyst being introduced at each succeeding point in the direction of flow, and proportioning the relative amounts oi unreactivated and reactivated catalyst introduced at the respective points to maintain an increasing catalytic activity in the direction of flow thereby establishing a substantially constant rate of reaction throughout the reaction zone despite said decreasing temperature. normally decreasing catalyst activity, and decreasing concentration of reactants.

2. A process for the endothermlc catalytic conversion of hydrocarbons which comprises vaporizing said hydrocarbons, passing the resultant vapors through an elongated reaction zone at conversion conditions oi temperature and pressure, such that the temperature decreases in the direction of ilow due to the endothermic reac tion, introducing powdered solid catalyst from two sources as hereinafter described into said reaction zone at a plurality of points spaced in the direction of flow for suspension in said vapors, separating conversion products from the eiiiuents of said reaction zone, separating and recycling insuiiiciently converted hydrocarbons, separating substantially all of the catalyst so introduced from the eilluents of said reaction zone, the thus-separated catalyst still retaining some activity. reactivating only a portion oi said separated catalyst, recycling the remainder of said separated catalyst without reactivation to a plurality of said points including the rst and excluding the last of said points in the direction of flow, the unreactivated catalyst introduced to said first point being the sole catalyst introduced thereto and a diminishing quantity of unreactivated catalyst being introduced at each succeeding point in the direction of ilow introducing the reactivated portion or said catalyst into the reaction zone at a plurality of points excluding the first and including the last of said points in the direction oi ow, the reactivated catalyst introduced to said last point being the sole catalyst introduced thereto and an increasing quantity oi' reactivated catalyst being introduced at each succeeding point in the direction of ow, and proportioning the relative amounts of unreactivated and reactivated catalyst introduced at the respective points to maintain an increasing catalytic activity in the direction of ow thereby establishing a substantially constant rate of reaction throughout the reaction zone despite said decreasing temperature, normally decreasing catalyst activity. and decreasing concentration of reactants.

3. A process for the endothermic catalytic conversion of hydrocarbons which comprises passing vapors of said hydrocarbons through an elongated reaction zone at conversion conditions of temperature and pressure, such that the temperature decreases in the direction of ilow due to the endotherxnic reaction, introducing powdered solid catalyst from two sources as hereinafter described into said reaction zone at a plurality of points spaced in the direction of ilow for suspension in said vapors, separating conversion products from the eiiiuents oi said reaction zone, separating substantially all of the catalyst so introduced from the eflluents of said reaction zone, the thus-separated catalyst still retaining some activity, reactivating only a portion o! said separated catalyst, recycling the remainder of said separated catalyst without reactivation to a plurality of said points including the ilrst and excluding the last o! said points in the 4direction oi now, the unreactivated catalyst introduced to 21 said first point being the sole catalyst introduced thereto and a diminishing quantity of unreactivated catalyst being introduced at each succeedlng point in the direction of 110W, introducing the reactivated portion of said catalyst into the reaction zone at a. plurality of points excluding the rst and including the last of said points in the direction of ow, the reactivated catalyst introduced to said last point being the soie catalyst introduced thereto and an increasing quantity of reactivated catalyst being` introduced at each succeeding point in the direction of ow, and. proportioning the relative amounts of unreaotivated and reactivated catalyst introduced at the respective points to maintain an increasing catalytic activity inthe direction of ilow thereby establishing a substantially constant rate of reaction throughont the reaction zone despite said decreasing temperature, normally decreasing cataiyst activity, and decreasing concentration of reactants.

THOMAS B. HUDSON.

REFERENCES CITED Number Number UNITED STATES PATENTS Name Date Lazier June 26, 1934 Delattre-Seguy Jan. 5, i937 Pier et al Nov. 30, 1937 Pier et al June 14, 1938 Peck June 13, 1939 Wiezeviclt Oct. 17, 1939 Pier et al. July 2, 1940 Marschner Sept. 3, 1940 Maranciir et al. Sept. 22, 1942 Thomas Oct. 27, 1942 Roberts et a1 Nov. 3, 1942 Watson Mar, 16, 1943 Day et al. Juif; 13, 1943 Egloi et al. l0, 1943 Nysewander Jen, 25, 1944 Danforth Feb. 22, 1944 Cornell June 25, 1946 FOREIGN PATENTS Country Date Great Britain June 4, 1934 Certiiicate el' Correction Patent No. 2,429,161.

THOMAS B. HUDSON It is hereby certified that errors appear in the numbered patent requiring correction es follows: Co

insert the; column 9, line 2, variable rates in" should read rates is; colnmn October 14, 1947.

rinted specification of the above umn 3, line 23, after surface of"- should read variables; column 12, line 38, 20, line 38, after the word How insert a comme; and that the said Letters Patent should be read with these corrections therein that the same may conform to the record of the case in the Patent Office.

Signed and sealed this 20th day of January, A. D. 1948.

THOMAS F. MURPHY,

21 said first point being the sole catalyst introduced thereto and a diminishing quantity of unreactivated catalyst being introduced at each succeedlng point in the direction of 110W, introducing the reactivated portion of said catalyst into the reaction zone at a. plurality of points excluding the rst and including the last of said points in the direction of ow, the reactivated catalyst introduced to said last point being the soie catalyst introduced thereto and an increasing quantity of reactivated catalyst being` introduced at each succeeding point in the direction of ow, and. proportioning the relative amounts of unreaotivated and reactivated catalyst introduced at the respective points to maintain an increasing catalytic activity inthe direction of ilow thereby establishing a substantially constant rate of reaction throughont the reaction zone despite said decreasing temperature, normally decreasing cataiyst activity, and decreasing concentration of reactants.

THOMAS B. HUDSON.

REFERENCES CITED Number Number UNITED STATES PATENTS Name Date Lazier June 26, 1934 Delattre-Seguy Jan. 5, i937 Pier et al Nov. 30, 1937 Pier et al June 14, 1938 Peck June 13, 1939 Wiezeviclt Oct. 17, 1939 Pier et al. July 2, 1940 Marschner Sept. 3, 1940 Maranciir et al. Sept. 22, 1942 Thomas Oct. 27, 1942 Roberts et a1 Nov. 3, 1942 Watson Mar, 16, 1943 Day et al. Juif; 13, 1943 Egloi et al. l0, 1943 Nysewander Jen, 25, 1944 Danforth Feb. 22, 1944 Cornell June 25, 1946 FOREIGN PATENTS Country Date Great Britain June 4, 1934 Certiiicate el' Correction Patent No. 2,429,161.

THOMAS B. HUDSON It is hereby certified that errors appear in the numbered patent requiring correction es follows: Co

insert the; column 9, line 2, variable rates in" should read rates is; colnmn October 14, 1947.

rinted specification of the above umn 3, line 23, after surface of"- should read variables; column 12, line 38, 20, line 38, after the word How insert a comme; and that the said Letters Patent should be read with these corrections therein that the same may conform to the record of the case in the Patent Office.

Signed and sealed this 20th day of January, A. D. 1948.

THOMAS F. MURPHY,

Aniston# onmm'oner of Patente. 

